CN112919610B - Fluidized bed reactor and catalyst unit for catalytic oxidation - Google Patents
Fluidized bed reactor and catalyst unit for catalytic oxidation Download PDFInfo
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- CN112919610B CN112919610B CN202011054204.5A CN202011054204A CN112919610B CN 112919610 B CN112919610 B CN 112919610B CN 202011054204 A CN202011054204 A CN 202011054204A CN 112919610 B CN112919610 B CN 112919610B
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- 239000003054 catalyst Substances 0.000 title claims abstract description 137
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 137
- 230000003647 oxidation Effects 0.000 title claims abstract description 89
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 70
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 70
- 239000002351 wastewater Substances 0.000 claims abstract description 26
- 238000003756 stirring Methods 0.000 claims abstract description 24
- 238000005273 aeration Methods 0.000 claims abstract description 21
- 238000005243 fluidization Methods 0.000 claims abstract description 20
- 238000007664 blowing Methods 0.000 claims abstract description 4
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 29
- 230000005484 gravity Effects 0.000 claims description 22
- 238000005192 partition Methods 0.000 claims description 12
- 239000000463 material Substances 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 3
- 238000013019 agitation Methods 0.000 claims description 2
- 238000005276 aerator Methods 0.000 claims 1
- 239000007789 gas Substances 0.000 description 22
- 239000010865 sewage Substances 0.000 description 18
- 239000000945 filler Substances 0.000 description 12
- 210000004027 cell Anatomy 0.000 description 10
- 238000013461 design Methods 0.000 description 5
- 238000000034 method Methods 0.000 description 4
- 238000003825 pressing Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000011001 backwashing Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000006378 damage Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000010842 industrial wastewater Substances 0.000 description 2
- 230000003068 static effect Effects 0.000 description 2
- 238000005299 abrasion Methods 0.000 description 1
- 238000009303 advanced oxidation process reaction Methods 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 210000005056 cell body Anatomy 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The present disclosure provides a fluidized bed reactor and a catalyst unit for catalytic oxidation. A fluidized bed reactor comprising a water inlet and an air inlet; an oxidation pond comprising an inner cavity for containing wastewater; the separator is arranged in the inner cavity of the oxidation pond along the vertical direction and divides the inner cavity into a catalytic oxidation reaction zone and a water outlet zone, a channel communicated with the catalytic oxidation reaction zone and the water outlet zone is formed between the separator and the bottom surface of the inner cavity, and the water inlet and the air inlet are positioned in the catalytic oxidation reaction zone and are communicated with the inner cavity; and a fluidization power supply unit arranged at a position far away from the separator in the catalytic oxidation reaction zone and used for blowing stirring gas into the oxidation pond. The stirring power is provided by a single-side aeration stirring mode, the circular stirring is formed, and the power consumption is low.
Description
Technical Field
The present disclosure relates to the field of wastewater treatment technologies, and in particular, to a fluidized bed reactor and a catalyst unit for catalytic oxidation.
Background
The refractory substances in the wastewater directly determine the standard discharge and stable operation of a sewage treatment plant, so the requirements of advanced treatment of refractory industrial wastewater and upgrading and reconstruction of municipal sewage are increasingly urgent. The traditional biochemical treatment method can not effectively remove toxic and harmful refractory substances in industrial wastewater, and the advanced oxidation process has the advantages of high efficiency, deep treatment degree and the like compared with the traditional biochemical treatment method. At present, the advanced oxidation technology adopted in the sewage treatment industry is mainly ozone catalytic oxidation, but in the traditional ozone catalytic oxidation technology, ozone enters a tank body and then continues to rise after passing through a catalyst layer, a large amount of ozone can only realize contact oxidation with sewage after passing through the catalyst layer, COD (Chemical Oxygen Demand) in the sewage is decomposed by utilizing the self-oxidizing property, the ozone loss is large, the utilization rate is low, the ozone concentration in tail gas is high, the environment is polluted, and in order to ensure the removal efficiency of the COD, the using amount of the catalyst and the adding amount of the ozone need to be increased, and the cost is high.
Disclosure of Invention
One of the objectives of the present disclosure is to provide a fluidized bed reactor for catalytic oxidation, which provides stirring power by means of single-side aeration stirring, and forms cyclic stirring, and has low power consumption.
According to an aspect of the present disclosure, there is provided a fluidized bed reactor for catalytic oxidation, comprising a water inlet and a gas inlet, the fluidized bed reactor comprising: an oxidation pond comprising an inner cavity for containing wastewater; the separator is arranged in the inner cavity of the oxidation pond along the vertical direction and divides the inner cavity into a catalytic oxidation reaction zone and a water outlet zone, a channel for communicating the catalytic oxidation reaction zone with the water outlet zone is formed between the separator and the bottom surface of the inner cavity, and the water inlet and the air inlet are positioned in the catalytic oxidation reaction zone and communicated with the inner cavity; and a fluidization power supply unit arranged at a position far away from the separator in the catalytic oxidation reaction zone and used for blowing stirring gas into the oxidation pond.
According to an embodiment of the present disclosure, the fluidized bed reactor may further include: and a plurality of catalyst units which are arranged in the catalytic oxidation reaction zone, wherein each catalyst unit is filled with a catalyst, the density of the catalyst unit in a wet-based state is slightly larger than that of the waste water, and the catalyst unit is fluidized under the action of the airflow provided by the fluidized power supply unit.
According to an embodiment of the present disclosure, the specific gravity of the catalyst unit in a wet-based state may be 1.03 to 1.05.
According to an embodiment of the present disclosure, the catalyst unit may include a housing and a catalyst, and form an eccentric body having a center of gravity close to one side.
According to an embodiment of the present disclosure, the case may be formed as a sphere, a pie, or a heteromorphic polyhedron, and the catalyst is filled in a lower portion of the case to form an eccentric sphere of a tumbler type.
According to the embodiment of the disclosure, the shell can be formed into a spherical body, the spherical body can be formed by an upper hemisphere and a lower hemisphere which are detachably connected, and the catalyst can be fixed in the lower hemisphere through the pressing sheet.
According to the embodiment of the disclosure, the shell may be formed into a sphere having a diameter of 8 to 10cm, the surface of the shell may be opened with a plurality of water passing holes having a diameter of 1 to 2mm, the surface of the shell has an aperture ratio of 40 to 80%, the shell is made of a material having a density less than that of the wastewater, the catalyst may be formed into a column shape of 3 to 5mmm, and a specific gravity of the catalyst is about 0.6 to 0.8.
According to an embodiment of the present disclosure, the fluidization power supply unit may include a gas stirring assembly disposed on a bottom surface of the oxidation tank at a position distant from the partition.
According to the embodiment of the disclosure, the gas stirring component can be a perforated aeration pipe, and the aeration gas-water ratio of the perforated aeration pipe is 4-10.
According to an embodiment of the present disclosure, the fluidized bed reactor may further include: and the water collecting weir is arranged in the water outlet zone, the top of the water collecting weir is higher than the liquid level of the water outlet zone by more than 10cm, an opening is formed on the side wall of the water collecting weir, and the aperture of the opening is designed to prevent the catalyst unit from passing through.
According to an embodiment of the present disclosure, the fluidized bed reactor may include a plurality of oxidation cells connected in series with each other, wherein the effluent zone of a previous oxidation cell of the plurality of oxidation cells is in communication with the catalytic oxidation reaction zone of a next oxidation cell.
According to another aspect of the present disclosure, there is provided a catalyst unit that may include a housing and a catalyst filled in the housing, and form an eccentric body having a center of gravity close to one side.
According to an embodiment of the present disclosure, the case may be formed as a sphere, a pie, or a heteromorphic polyhedron, and the catalyst is filled in a lower portion of the case to form an eccentric sphere of a tumbler type.
According to an embodiment of the present disclosure, the housing may be formed as a sphere composed of an upper hemisphere and a lower hemisphere detachably connected, and the catalyst is fixed in the lower hemisphere by a tablet.
According to the embodiment of the present disclosure, the housing may be formed in a sphere having a diameter of 8 to 10cm, the surface of the housing may be opened with a plurality of openings having a diameter of 1 to 5mm, the surface of the housing has an opening ratio of 40 to 80%, the housing is made of a material having a density lower than that of the wastewater, the catalyst is formed in a column shape of 3 to 5mmm, the specific gravity of the catalyst is about 0.6 to 0.8, and the specific gravity of the catalyst unit in a wet state is 1.03 to 1.05.
The oxidation pond is divided into a left area and a right area by the partition, and the fluidization power supply unit is arranged at the bottom of the catalytic oxidation reaction area and is positioned at one side far away from the partition, so that circular stirring is formed in the catalytic oxidation reaction area, and the power consumption is low; and the catalyst unit can be fluidized under the action of the airflow provided by the fluidized power supply unit, so that three-phase contact of the wastewater, the ozone and the catalyst in the catalyst unit is realized, and the catalytic oxidation reaction efficiency is improved.
Drawings
The above and/or other objects and advantages of the present disclosure will become more apparent from the following description of the embodiments taken in conjunction with the accompanying drawings, in which:
fig. 1 is a schematic diagram of a fluidized bed reactor for catalytic oxidation in an exemplary embodiment of the present disclosure.
Fig. 2 is a schematic diagram of the catalyst unit in fig. 1.
Fig. 3 is an exploded schematic view of the catalyst unit in fig. 2.
Fig. 4 is a schematic view of a pellet included in the catalyst unit of fig. 2.
The reference numbers illustrate:
1: oxidation pond, 11: catalytic oxidation reaction zone, 12: water outlet zone, 13: a channel, 2: separator, 3: fluidization power supply unit, 4: catalyst unit, 41: a housing, 42: water passing hole, 43: upper hemisphere, 44: lower hemisphere, 45: tabletting, 5: a water collecting weir.
Detailed Description
Hereinafter, a fluidized bed reactor and a catalyst unit according to exemplary embodiments of the present disclosure will be described in detail with reference to the accompanying drawings. Like reference numerals refer to like parts throughout the drawings.
It will be understood that the use of the terms first, second, etc. may not denote any order or importance, but rather the terms first, second, etc. may be used to distinguish one element from another.
As shown in fig. 1, a fluidized bed reactor for catalytic oxidation of an exemplary embodiment of the present disclosure includes: an oxidation pond 1 comprising an inner cavity for accommodating wastewater; a water inlet and a gas inlet for introducing wastewater and gas (e.g., ozone) into the oxidation basin 1; the separator 2 is arranged in the inner cavity of the oxidation pond 1 along the vertical direction, and divides the inner cavity of the oxidation pond 1 into a catalytic oxidation reaction zone 11 and a water outlet zone 12, a channel 13 for communicating the catalytic oxidation reaction zone 11 with the water outlet zone 12 is formed between the separator 2 and the bottom surface of the inner cavity, and a water inlet and a gas inlet are positioned in the catalytic oxidation reaction zone 11 and are communicated with the inner cavity; and a fluidization power supply unit 3 disposed at a position of the catalytic oxidation reaction zone 11 away from the partition 2 for blowing stirring gas into the oxidation cell 1.
While the conventional method of introducing the stirring gas in the vertical direction and forming the circulating fluidization in the inner and outer sleeves requires a high upward flow velocity and requires a differential velocity between the inner and outer hydraulic flow velocities, so that the circulation is ensured, the power consumption is high, the fluidized bed reactor according to the exemplary embodiment of the present disclosure divides the oxidation tank 1 into two regions (i.e., the catalytic oxidation reaction region 11 and the water outlet region 12) on the left and right by the partition 2, and the fluidization power supply unit 3 is formed at the bottom of the catalytic oxidation reaction region 11 and on the side away from the partition 2, so that the circulating stirring is formed in the catalytic oxidation reaction region 11, and the power consumption is low.
The oxidation pond 1 may be formed in a rectangular parallelepiped shape, but the present disclosure is not limited thereto, and may be formed in a special cube having a trapezoidal cross section. The partition 2 may be plate-shaped, i.e. form a flow guide matching the cross-sectional shape of the inner cavity. The guide plate extends from one side wall of the oxidation tank 1 to the opposite side wall in the horizontal direction, and extends from the upper part of the oxidation tank 1 to the bottom surface of the oxidation tank 1 in the vertical direction to divide the oxidation tank 1 into the catalytic oxidation reaction zone 11 and the water outlet zone 12, and the lower part of the guide plate may be slightly higher than the bottom surface of the inner cavity to form a passage 13 communicating the catalytic oxidation reaction zone 11 and the water outlet zone 12 with the bottom surface of the oxidation tank 1, so that the sewage can enter the water outlet zone 12 from the catalytic oxidation reaction zone 11 through the passage 13, but the catalyst unit 4 is not easy to pass through the passage 13. The present disclosure is not limited thereto and an opening may be formed at a lower portion of the partition 2 to form a passage 13 communicating the catalytic oxidation reaction zone 11 and the water outlet zone 12.
The water inlet of the fluidized bed reactor can be communicated with a water source and is used for introducing wastewater (sewage) into the oxidation pond 1. The air inlet of the fluidized bed reactor can be communicated with an ozone generator and is used for introducing ozone. The fluidized bed reactor according to an exemplary embodiment of the present disclosure may further include a gas-water mixer (not shown) which is communicated with the water inlet and the gas inlet of the fluidized bed reactor, and a mixture outlet of the gas-water mixer may be communicated with the inner cavity of the oxidation tank 1, and ozone and wastewater may be mixed by the gas-water mixer (not shown) and then fed into the oxidation tank 1 together. Therefore, the catalytic oxidation reaction zone 11 of the oxidation cell 1 can be regarded as a water inlet side, and the water outlet zone 12 can be regarded as a water outlet side.
The traditional ozone catalytic oxidation technology is mainly a fixed bed process, a catalyst is static in a reactor, the thickness of a catalyst layer of the fixed bed is very small, the catalyst layer accounts for a very small proportion of the height of the reactor, and the ozone cannot be catalyzed completely to generate hydroxyl radicals, so that a large amount of ozone can only be in contact oxidation with sewage after passing through the catalyst layer, and COD in the sewage is decomposed by utilizing the self-oxidation. And the fluidized bed reactor according to the exemplary embodiment of the present disclosure further includes a plurality of catalyst units 4 disposed in the catalytic oxidation reaction zone 11, each of the catalyst units 4 being filled with a catalyst, and the catalyst units 4 having a density in a wet-based state slightly greater than that of the wastewater, so that the catalyst units 4 can be fluidized by the gas flow provided by the fluidizing power supply unit 3. That is, in order to improve the efficiency of the catalytic oxidation reaction in the oxidation pond 1, the fluidized power supply unit 3 forms a fluidized bed in the oxidation pond 1, the catalyst unit 4 is in a fluidized state in the oxidation pond 1, three-phase contact between the wastewater, the ozone and the catalyst in the catalyst unit 4 is realized, and before the ozone overflows from the sewage, the catalytic reaction can be realized, a large amount of hydroxyl radicals are generated, so that the efficiency of the catalytic oxidation reaction is improved, the using amount of the catalyst, the adding amount of the ozone and the concentration of the ozone in the tail gas can be reduced, the pressure of tail gas damage is reduced, and the risk of tail gas pollution is also reduced.
The density of the catalyst unit 4 in the wet-based state is slightly larger than that of the wastewater, so that the catalyst unit 4 can be deposited at the bottom of the oxidation tank 1 under the action of gravity of the wastewater in a static state (for example, without aeration or stirring) of the wastewater, and the catalyst unit 4 can be in a suspended motion state in the wastewater and circularly flow in the catalytic oxidation reaction zone 11 under the stirring and aeration actions of the fluidized power supply unit 3, so that the contact area with ozone and sewage is increased, and the catalytic oxidation reaction efficiency is increased. In addition, due to the high density of the catalyst units 4 of the present disclosure, a majority of the catalyst units 4 circulate within the catalytic oxidation reaction zone 11 without entering the effluent zone 12, i.e., a small amount enters the effluent zone 12 and a majority of the catalyst units are deposited on the bottom of the tank. Wherein, if the density of the catalyst unit 4 in the wet state is too high, the fluidization power supply unit 3 cannot or is difficult to realize fluidization; if the density is less than that of the wastewater, the catalyst unit 4 floats to the surface of the wastewater, causing the catalyst therein to fail to effectively contact ozone. In an embodiment, the specific gravity of the catalyst unit 4 in a wet state may be 1.03 to 1.05. The catalyst unit 4 can be filled in a filling ratio of 20-60% of the volume of the oxidation pond 1, and the space velocity of the catalyst can be more than 10.
According to an exemplary embodiment of the present disclosure, the fluidization power supply unit 3 may include a gas stirring assembly. The gas stirring assembly may be disposed on the bottom surface of the oxidation tank 1 at a position distant from the partition 2, for example, at a position close to the left side wall of the oxidation tank 1 as in fig. 1. In an embodiment, the gas agitation assembly may include a perforated aeration pipe arranged at the bottom of the oxidation tank 1 in parallel with the extending direction of the partition 2, the perforated aeration pipe having a plurality of aeration openings formed therein, and an inlet thereof communicating with the blower and the aeration device through an air intake pipe. According to the present disclosure, the design of single-side aeration is adopted, so that the single-side hydraulic stirring strength in the oxidation pond 1 can be enhanced, the fluidization of the catalyst unit 4 is realized, and the wastewater in the catalytic oxidation reaction zone 11 forms a circulating flow state through the flow guiding effect of the separator 2, so that the catalyst unit 4 is promoted to circularly move in the catalytic oxidation reaction zone 11 along the clockwise direction in fig. 1, and the catalytic oxidation reaction efficiency is increased.
Wherein, the specific aeration mode of the perforated aeration pipe can be small resistance perforated aeration, the resistance loss of the small resistance perforated aeration pipe is about 300mm, the aeration gas-water ratio of the perforated aeration pipe can be 4-10, so as to strengthen the single-side hydraulic stirring intensity in the tank body and realize the fluidization of the catalyst unit 4, but not limited to the above.
The catalyst unit 4 may include a case 41 and a catalyst filled in the case 41. Wherein, the housing 41 may be formed as a sphere, a pie, or a heteromorphic polyhedron.
As shown in fig. 2 and 3, the housing 41 may be formed as a sphere body, and the sphere body is constructed of two parts of an upper hemisphere 43 and a lower hemisphere 44, which are detachably coupled. Due to the fact that the split type design is adopted, the split type catalyst filling device is divided into an upper portion and a lower portion, the upper portion and the lower portion can be connected together through clamping grooves and the like, the shell 41 is guaranteed to be easily disassembled and can be fastened after the catalyst is filled, the catalyst can be conveniently filled in the shell 41, and the catalyst can be prevented from leaking from the shell 41. The present disclosure is not limited thereto and the housing 41 may be formed as a hollow, unitary spherical body.
The housing 41 may be made of a light material, for example, a filler ball made of a filler having a density lower than that of the waste water, so that the catalyst may be weighted, the overall specific gravity of the filler ball may be changed, and additional design of a filler such as foam may not be required to achieve the weighting. In addition, the housing 41 may be made of an oxidation-resistant material that is not sensitive to oxidation by ozone, so as to prevent oxidation corrosion by ozone.
The housing 41 may be opened with a plurality of water holes 42 so that the waste water may contact the catalyst. The number and the hole diameter of the water through holes 42 on the surface of the housing 41 need to be designed in consideration of the water through rate so as to increase the contact probability between the catalyst and the sewage, and simultaneously, the catalyst in the housing 41 needs to be prevented from leaking and escaping. In an embodiment, the casing 41 may be a sphere with a diameter of 8-10 cm, the surface of the casing 41 is opened with a plurality of water holes 42 with a diameter of 1-2 mm, and the opening ratio of the surface of the casing 41 is 40-80%. The catalyst may be formed in a columnar shape of 3 to 5mmm and the specific gravity of the catalyst is about 0.6 to 0.8, so that the specific gravity of the assembly as a whole in a wet state is ensured to be 1.03 to 1.05 after the catalyst is filled in the above-mentioned case 41.
In the traditional ozone reactor, the catalyst is easy to adhere and suspend, so that the problem of catalyst pollution and efficiency reduction is caused, and the catalyst disclosed by the invention is always in a fluidized state in the tank body and repeatedly collides and rubs, so that the pollution is avoided. However, it is because the catalyst unit 4 is fluidized at a high speed in the case where a fluidized bed is formed in the oxidation tank 1, in which the catalyst collides and rubs in the housing 41, causing abrasion of the catalyst. In order to reduce the catalyst breakage rate and the catalyst replenishment rate, the catalyst unit 4 according to the disclosed exemplary embodiment is formed as an eccentric body with the center of gravity on one side. Specifically, the catalyst may be filled in a lower portion of the housing 41 to form an eccentric sphere in a tumbler type.
Further, after the catalyst is loaded into the housing 41, the catalyst may be fixed to the lower portion of the housing 41 by the pressing sheet 45 as shown in fig. 4. Since the center of gravity of the entire catalyst unit 4 is located at the lower portion, when the catalyst unit 4 is fluidized, it is ensured that the catalyst inside the casing 41 is relatively stationary and always located at the lower portion, and does not tumble, and the friction of the catalyst in the casing 41 can be reduced to the maximum extent. The pressing sheet 45 can form the function of pressing the catalyst by using the principle of a buckle, and the catalyst is ensured to be arranged on the lower half part of the shell 41. The present disclosure is not limited thereto as long as the catalyst can be fixed at a desired position within the housing 41 such that the fixed housing 41 and the catalyst form an eccentric body.
As shown in fig. 1, the filler balls are all suspended under the action of the hydraulic stirring and aeration pipelines and simultaneously circulate in the body of the oxidation tank 1 under the action of the water flow, but most of the filler balls are isolated in the catalytic oxidation reaction zone 11 due to the obstruction of the flow guide plate, if some of the filler balls enter the water outlet zone 12 from the bottom of the flow guide plate, the fluidized bed reactor can also comprise a water collecting weir 5 arranged in the water outlet zone 12 according to the exemplary embodiment of the present disclosure. The top of the water collection weir 5 can be higher than the liquid level of the water outlet zone 12 by more than 10cm, the side wall of the water collection weir 5 is provided with an opening, and the aperture of the opening is designed to be smaller than the size of the catalyst unit 4, so that the catalyst unit 4 can not pass through, and the filler balls and the sewage can be effectively separated. The aperture of the opening on the water collecting weir 5 can be 5-6 cm in size, so that sewage can pass through but the filler balls are blocked due to the larger diameter (8-10 cm diameter). According to the exemplary embodiment of the present disclosure, by providing the water collection weir 5, it is possible to ensure uniform water outlet on one side of the guide plate, and to effectively intercept the suspended filler balls, thereby achieving effective separation of the filler balls from the sewage.
In addition, the top of oxidation pond 1 is provided with sealed lid, and fluidized bed reactor still can include tail gas collection processing apparatus, and tail gas collection processing apparatus can be connected to catalytic oxidation reaction zone 11 for retrieve the tail gas of catalytic oxidation reaction zone 11 and carry out destruction processing, discharge after reaching standard again, in order to avoid air pollution.
As an example, the fluidized bed reactor may include a plurality of oxidation cells 1, for example, three oxidation cells 1, connected in series with each other. The effluent area 12 of the last oxidation pond 1 in the plurality of oxidation ponds 1 is communicated with the catalytic oxidation reaction area 11 of the next oxidation pond 1.
Specifically, in an example, the fluidized bed reactor may include three oxidation cells and a degassing cell arranged in series along a water flow direction. Wherein, the three oxidation ponds have the structure and the components of the oxidation pond 1 as described above, that is, each oxidation pond 1 is divided into a catalytic oxidation reaction zone 11 and a water outlet zone 12 by a partition 2 and is provided with a fluidization power supply unit 3 and the like for fluidizing a plurality of catalyst units 4, which will not be described in detail herein. Wherein, the water inlet and the air inlet of the fluidized bed reactor are communicated with the inner cavity of the first oxidation pond 1.
Another aspect of the present disclosure provides a catalyst unit 4 including a case 41 and a catalyst filled in the case 41, and forming an eccentric body having a center of gravity close to one side. With respect to the catalyst unit 4, the above has been described in detail, and the description thereof is omitted.
According to the fluidized bed reactor disclosed by the embodiment of the disclosure, the stirring power is provided in a single-side aeration mode, the fluidized state of the oxidation tank is realized, the catalytic oxidation efficiency of ozone is higher than that of the existing fixed bed reactor, the contact area and the contact time of ozone, sewage and the catalyst are increased, and the one-time investment cost and the ozone consumption cost of the catalyst are reduced. Wherein, fluidized bed reactor is at the operation in-process, through the cooperation of separator and fluidization power supply unit for the catalyst is in fluidization state and is circulated the fluidization in the cell body, forms the three-phase contact with sewage and ozone in the pond, therefore reaction efficiency is higher, according to different quality of water, the height of reactor can be optimized, reduces the civil engineering cost.
According to the fluidized bed reactor disclosed by the embodiment of the disclosure, the design of the reactor is simplified, a water distribution device is not required to be additionally designed, and the catalytic oxidation reaction can be realized in the whole flow due to the higher efficiency of the catalyst of the fluidized bed reactor, so that the height of the reactor can be greatly reduced, and the water collection weir 5 at the top of the pool can also be greatly reduced.
According to the fluidized bed reactor disclosed by the embodiment of the disclosure, the filter head, the filter plate, the water distribution system, the backwashing gas distribution system and the backwashing system of the conventional fixed bed reactor are eliminated through the design of the reactor, and the absolute mixing of the catalyst and the sewage in the pool body is ensured, so that no dead angle exists, the reaction efficiency is greatly improved, and the complexity and the investment cost of the reactor are greatly reduced.
According to the catalyst unit of the embodiment of the disclosure, after the catalyst is filled, the gravity center is inclined to the lower part and is in an eccentric state, so that the catalyst unit does not roll violently under the action of gravity in the tank body, but can move continuously, the relative displacement and friction of the catalyst in the filler ball are reduced to the maximum extent, the catalyst is prevented from being broken, and the replenishment rate is reduced.
The above description is only a preferred embodiment of the present disclosure, but the scope of the present disclosure is not limited thereto, and any changes or substitutions (e.g., combinations of features in different embodiments of the present disclosure) that can be easily conceived by a person skilled in the art within the technical scope of the present disclosure should be included in the scope of the present disclosure. Therefore, the protection scope of the present disclosure shall be subject to the protection scope of the claims.
Claims (15)
1. A fluidized bed reactor for catalytic oxidation comprising a water inlet and a gas inlet, characterized in that the fluidized bed reactor comprises:
an oxidation pond (1) comprising an inner cavity for containing waste water;
the separator (2) is arranged in the inner cavity of the oxidation pond (1) along the vertical direction and divides the inner cavity into a catalytic oxidation reaction zone (11) and a water outlet zone (12), a channel (13) for communicating the catalytic oxidation reaction zone (11) with the water outlet zone (12) is formed between the separator (2) and the bottom surface of the inner cavity, the water inlet and the air inlet are positioned in the catalytic oxidation reaction zone (11) and communicated with the inner cavity, and the air inlet is used for introducing ozone; and
a fluidization power supply unit (3) which is arranged at the position of the catalytic oxidation reaction zone (11) far away from the separator (2) and is used for blowing stirring gas into the oxidation pond (1);
a plurality of catalyst units (4) arranged in the catalytic oxidation reaction zone (11), wherein the lower part of the separator (2) is slightly higher than the bottom surface of the inner cavity, so that the catalyst units (4) cannot easily enter the water outlet zone (12).
2. Fluidized bed reactor for catalytic oxidation according to claim 1,
each catalyst unit (4) is filled with a catalyst, and the catalyst unit (4) has a density slightly higher than that of the wastewater in a wet state and is fluidized by the gas flow provided by the fluidization power supply unit (3).
3. Fluidized bed reactor for catalytic oxidation according to claim 2, characterized in that the specific gravity of the catalyst unit (4) in the wet-based state is 1.03-1.05.
4. Fluidized bed reactor for catalytic oxidation according to claim 1, characterized in that the catalyst unit (4) comprises a housing (41) and the catalyst and forms an eccentric body with a centre of gravity close to one side.
5. Fluidized bed reactor for catalytic oxidation according to claim 4, characterized in that the housing (41) is formed as a sphere, a pie or a heteromorphic polyhedron, and the catalyst is filled in the lower part of the housing (41) to form an eccentric sphere of a tumbler type.
6. Fluidized bed reactor for catalytic oxidation according to claim 5, characterized in that the housing (41) is formed as a sphere consisting of an upper hemisphere (43) and a lower hemisphere (44) detachably connected, the catalyst being fixed inside the lower hemisphere by a tablet (45).
7. The fluidized bed reactor for catalytic oxidation according to claim 6, wherein the housing (41) is formed as a sphere having a diameter of 8 to 10cm, the surface of the housing (41) is opened with a plurality of water passing holes (42) having a hole diameter of 1 to 2mm, the surface of the housing (41) has an open porosity of 40 to 80%, the housing (41) is made of a material having a density lower than that of the wastewater, the catalyst is formed in a columnar shape of 3 to 5mmm, and the specific gravity of the catalyst is 0.6 to 0.8.
8. Fluidized bed reactor for catalytic oxidation according to claim 1, characterized in that the fluidization power supply unit (3) comprises a gas stirring assembly arranged on the bottom surface of the oxidation basin (1) at a position remote from the partition (2).
9. The fluidized bed reactor for catalytic oxidation according to claim 8, wherein the gas agitation assembly is a perforated aerator pipe having an aeration gas-water ratio of 4 to 10.
10. The fluidized bed reactor for catalytic oxidation according to claim 2, characterized in that it further comprises: and the water collection weir (5) is arranged in the water outlet zone (12), the top of the water collection weir (5) is higher than the liquid level of the water outlet zone (12) by more than 10cm, an opening is formed on the side wall of the water collection weir (5), and the diameter of the opening is designed to prevent the catalyst unit (4) from passing through.
11. Fluidized bed reactor for catalytic oxidation according to any of the claims 1 to 10, characterized in that it comprises a plurality of said oxidation cells (1) connected in series with each other, wherein the effluent zone (12) of a previous oxidation cell (1) of said plurality of oxidation cells (1) communicates with the catalytic oxidation reaction zone (11) of a next oxidation cell (1).
12. A catalyst unit, characterized in that the catalyst unit (4) comprises a housing (41) and a catalyst filled in the housing (41) and forms an eccentric body with the center of gravity close to one side, and the catalyst is filled in the lower part of the housing (41) to form an eccentric sphere of a tumbler type.
13. A catalyst unit according to claim 12, characterized in that the housing (41) is formed as a sphere, a pie or a heteromorphic polyhedron.
14. A catalyst unit according to claim 12, characterised in that the housing (41) is formed as a sphere consisting of an upper hemisphere and a lower hemisphere detachably connected, the catalyst being fixed in the lower hemisphere by a tablet.
15. The catalyst unit according to claim 12, wherein the case (41) is formed as a sphere having a diameter of 8 to 10cm, the case (41) has a surface opened with a plurality of openings having a diameter of 1 to 5mm, the case (41) has a surface opening ratio of 40 to 80%, the case (41) is made of a material having a density lower than that of wastewater, the catalyst is formed in a columnar shape having a density of 3 to 5mmm, the catalyst has a specific gravity of 0.6 to 0.8, and the catalyst unit (4) has a specific gravity of 1.03 to 1.05 in a wet basis state.
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| CN101219831A (en) * | 2008-01-25 | 2008-07-16 | 北京工业大学 | Migration bed/activated sludge process series arrangement |
| CN201510885U (en) * | 2009-12-08 | 2010-06-23 | 中国科学院山西煤炭化学研究所 | Material box for catalyst cyclic regeneration |
| CN103193314B (en) * | 2013-05-03 | 2014-04-30 | 哈尔滨工业大学 | Sludge self-circulation dispersed sewage treatment device applicable to sewage reuse and method thereof |
| CN104556347A (en) * | 2014-12-15 | 2015-04-29 | 浙江中凯瑞普环境工程股份有限公司 | Wastewater treatment catalytic ozonation reactor for fluidized bed and wastewater treatment method of wastewater treatment catalytic ozonation reactor |
| CN106976954A (en) * | 2017-03-31 | 2017-07-25 | 北京首创清源环境科技有限公司 | A kind of eccentric filler |
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